US3888970A - Double layer catalyst bed for removing so' 2 'from waste gases - Google Patents
Double layer catalyst bed for removing so' 2 'from waste gasesDownload PDFInfo
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- US3888970A US3888970AUS331726AUS33172673AUS3888970AUS 3888970 AUS3888970 AUS 3888970AUS 331726 AUS331726 AUS 331726AUS 33172673 AUS33172673 AUS 33172673AUS 3888970 AUS3888970 AUS 3888970A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
- B01J8/0449—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds
- B01J8/0453—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds the beds being superimposed one above the other
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/74—Iron group metals
- B01J23/745—Iron
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
- B01J8/0476—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more otherwise shaped beds
- B01J8/0488—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more otherwise shaped beds the beds being placed in separate reactors
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
- C01B17/0473—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by reaction of sulfur dioxide or sulfur trioxide containing gases with reducing agents other than hydrogen sulfide
- C01B17/0486—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by reaction of sulfur dioxide or sulfur trioxide containing gases with reducing agents other than hydrogen sulfide with carbon monoxide or carbon monoxide containing mixtures
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/02—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles
- B01J2208/023—Details
- B01J2208/024—Particulate material
- B01J2208/025—Two or more types of catalyst
Definitions
- First layerconsists of iron, chromium, nickel, manganese, or cobalt, supported on alumina.
- Second layerconsists of alumina.
- This inventionrelates to the removal of sulfur dioxide from waste gases.
- Sulfur dioxideis a constituent of many waste gases, including gases from l fossil fuel (e.g., coal) burners, (2) sulfide ore processing as roasters, smelters and converters, (3) sour petroleum gas refineries, (4) paper mills, and (5) sulfuric acid manufacturing plants. Even though present in low concentration, the sulfur oxides contaminate the atmosphere, and must be removed in order to prevent adverse effects on human life, plant life, building materials, etc.
- catalytic reduction bedshave previously been used for producing sulfur from S0 I-Ieretofore, the most effective bed constituted a metal such as iron supported on alumina.
- Our inventioncomprises passing a dry SO containing gas through a single catalytic bed composed of two layers of different catalysts, the first layer of which consists of a metal such as iron, chromium, or nickel, supported on y-alumina, while the second layer consists of 'y-alumina.
- a catalyst bed temperature of about 400Cis employed. SO containing gas enters the bed through the first layer and product gas leaves the bed from the second layer.
- the double-layer bed of the present inventioncan result in a product gas containing less than /a the amount of gaseous sulfur compounds.
- Another objectis to catalytically convert said S0 to S.
- a further objectis to effect said conversion in a double-layer bed.
- FIG. 1illustrates a double-layer bed
- FIG. 2is a graph comparing the present invention with the prior art.
- FIG. 3is a modification of FIG. 1.
- reference numeral 1designates a reactor tube containing a packed catalyst bed composed of two layers 2 and 3.
- Layer 2consists of metal supported on y-alumina while layer 3 consists of y-alumina.
- the following metals (supported on alumina)are suitable for layer 2: Fe, Cr, Ni, Co, or Mn. Iron is preferred.
- Dry, CO-, SO -containing gasenters the bed through conduit 4, passes first through layer 2, then through layer 3, and product gas exits from the bed through conduit 5.
- the bedis preferably made up of pellets.
- a heater or furnace 6heats the reactor tube to the operating temperature (about 400C).
- Gaseous elemental sulfuris removed from the product gas in the prior art manner (e.g., condensation).
- S0 and COpreferably are present in the feed gas in a COzSO mole ratio of 2:1.
- inert constituentsother compounds such as CO (at 20 percent) or 0 (at 0.5 percent) can also be present.
- Nitrogen and other inert gasesexert no deleterious effects. Small quantities of higher oxides of sulfur and nitrogen can simultaneously be reduced on the catalyst. Optimum gas throughputs are best determined experimentally.
- Iron alumina catalystwas prepared by pelletizing a mixture of minus 10 micron ferric oxide and minus 0.05 micron gamma alumina into minus l6-plus 20- mesh pellets. The pellets were indurated at 1,200C for 2 hours and reduced at 600C for 1 hour with hydrogen. A two-gram sample of the catalyst (ferric oxide was completely reduced) was placed in reactor tubes, and a gas containing 4.7 vol. S0 10% CO (the remainder nitrogen) was passed over the sample at varying temperatures. The percentage of gaseous sulfur compounds in the product gas was determined and plotted against reactor temperature. The results are shown in curve a of FIG. 2.
- EXAMPLE 2In a second series of tests one gram of the pelletized catalyst as prepared in example I was placed in a reactor tube. In addition, 1 gram of 0.05 micron gamma alumina, which had been pelletized into minus l6-plus 20-mesh size was also placed in the same reactor tube forming a dual-layer bed of catalyst as shown in FIG. 1. A gas having the same composition as shown in example l was passed through the bed at varying temperatures. The results are shown as curve b in FIG. 2.
- the gaseous sulfur compounds in the feed gasare reduced to minimal concentration by the catalyst bed of the present invention at a temperature of about 400C, while a single-layer iron-alumina catalyst bed requires temperatures above 550C to even approach minimal concentration.
- FIG. 3therein is shown a further modification of the present invention wherein a dry gas in conduit 7 containing little or no CO is passed through a coke bed 8 at a temperature of about 500C to produce the necessary CO for the catalysis in the dual-layer bed in reactor tube 1.
- the first layer of the dual-layer bedfavors the rapid production of sulfide intermediates, which rapidly react to form elemental sulfur in the presence of the catalyst in the second layer, although the improved results of the present invention are not attained when the pellets of the two layers are intimately intermixed.
- a process for removing $0 from a dry waste gascomprising passing said waste gas through a single bed of catalyst said bed having a temperature of about 400C in the presence of CO; said CO and S0 being present in a COzSO mole ratio of at least 2:1; said bed consisting of a first and second layer of catalyst, said first layer consisting of iron, chromium, nickel, cobalt about 500C so as to produce said CO.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Materials Engineering (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Inorganic Chemistry (AREA)
- Catalysts (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
Description
[ June 10, 1975 Thumm et al. Watson et s ak Mu B 75 2 5677 9999lll W804 1 6593 55 3 ,92 5953 89 5 2333 DOUBLE LAYER CATALYST BED FOR REMOVING S0 FROM WASTE GASES [75] Inventors: Larry A. Haas, Burnsville; Sanaa E. Khalafalla; Thomas H. McCormick, both of Minneapolis, all of Minn.
The United States of America as [73] Assignee: Primary Examiner0scar R. Wertiz represented by the Secretary of the Assistant Examiner-Brian E. Hearn Interior, Washington, DC.
Feb. 12, 1973 Appl. No.: 331,726
[22] Filed:
ABSTRACT 52 Us.423/ 244;423/569;423/570 51 Int.Cl.B01d 53/34;C01b 17/04 DryWaste gas contammg 2 and C0 18 Passed [58] Field of Search 423/570, 569, 567, 242, thmugh double layer bed f Catalyst at 400C First layer consists of iron, chromium, nickel, manganese, or cobalt, supported on alumina. Second layer consists of alumina.
[56] References Cited UNITED STATES PATENTS 2,631,921 3/1953 Odell 423/659 6 Claims, 3 Drawing Figures PATENTEDJUH 10 I975 (PRIOR ART) IRON IN ALUMINA CATALYST OF PRESENT INVENTION O 5. l. O
TEMPERATURE c DOUBLE LAYER CATALYST BED FOR REMOVING SO FROM WASTE GASES This invention relates to the removal of sulfur dioxide from waste gases.
Sulfur dioxide is a constituent of many waste gases, including gases from l fossil fuel (e.g., coal) burners, (2) sulfide ore processing as roasters, smelters and converters, (3) sour petroleum gas refineries, (4) paper mills, and (5) sulfuric acid manufacturing plants. Even though present in low concentration, the sulfur oxides contaminate the atmosphere, and must be removed in order to prevent adverse effects on human life, plant life, building materials, etc.
Present commercial methods for removinglow concentrations 5%) of sulfur dioxide from waste gases involve two steps: 1) adsorption in bulky solids or liquids, and (2) desorption and regeneration of the sorbent.
Additionally, catalytic reduction beds have previously been used for producing sulfur from S0 I-Ieretofore, the most effective bed constituted a metal such as iron supported on alumina.
We have now developed a new and improved catalytic bed. Our invention comprises passing a dry SO containing gas through a single catalytic bed composed of two layers of different catalysts, the first layer of which consists of a metal such as iron, chromium, or nickel, supported on y-alumina, while the second layer consists of 'y-alumina. With CO as a reductant, a catalyst bed temperature of about 400C is employed. SO containing gas enters the bed through the first layer and product gas leaves the bed from the second layer.
In comparison to the product gas ofa bed of iron supported on alumina at an operating temperature of 400C, the double-layer bed of the present invention can result in a product gas containing less than /a the amount of gaseous sulfur compounds.
It is therefore an object of the present invention to remove S0 from a waste gas.
Another object is to catalytically convert said S0 to S.
A further object is to effect said conversion in a double-layer bed.
Other objects and advantages will be obvious from the following more detailed description of the invention taken in conjunction with the drawings in which:
FIG. 1 illustrates a double-layer bed;
FIG. 2 is a graph comparing the present invention with the prior art; and
FIG. 3 is a modification of FIG. 1.
Referring to the FIG. 1,reference numeral 1 designates a reactor tube containing a packed catalyst bed composed of twolayers Layer 2 consists of metal supported on y-alumina whilelayer 3 consists of y-alumina. The following metals (supported on alumina) are suitable for layer 2: Fe, Cr, Ni, Co, or Mn. Iron is preferred. I
Dry, CO-, SO -containing gas enters the bed throughconduit 4, passes first throughlayer 2, then throughlayer 3, and product gas exits from the bed throughconduit 5. The bed is preferably made up of pellets. A heater or furnace 6 heats the reactor tube to the operating temperature (about 400C).
Gaseous elemental sulfur is removed from the product gas in the prior art manner (e.g., condensation).
S0 and CO preferably are present in the feed gas in a COzSO mole ratio of 2:1. Besides inert constituents, other compounds such as CO (at 20 percent) or 0 (at 0.5 percent) can also be present. Nitrogen and other inert gases exert no deleterious effects. Small quantities of higher oxides of sulfur and nitrogen can simultaneously be reduced on the catalyst. Optimum gas throughputs are best determined experimentally.
Most efficient utilization of the bed constituents is attained whenlayers
The following example compares the catalyst bed of the present invention with the prior art.
EXAMPLE 1 Iron alumina catalyst was prepared by pelletizing a mixture of minus 10 micron ferric oxide and minus 0.05 micron gamma alumina into minus l6-plus 20- mesh pellets. The pellets were indurated at 1,200C for 2 hours and reduced at 600C for 1 hour with hydrogen. A two-gram sample of the catalyst (ferric oxide was completely reduced) was placed in reactor tubes, and a gas containing 4.7 vol. S0 10% CO (the remainder nitrogen) was passed over the sample at varying temperatures. The percentage of gaseous sulfur compounds in the product gas was determined and plotted against reactor temperature. The results are shown in curve a of FIG. 2.
EXAMPLE 2 In a second series of tests one gram of the pelletized catalyst as prepared in example I was placed in a reactor tube. In addition, 1 gram of 0.05 micron gamma alumina, which had been pelletized into minus l6-plus 20-mesh size was also placed in the same reactor tube forming a dual-layer bed of catalyst as shown in FIG. 1. A gas having the same composition as shown in example l was passed through the bed at varying temperatures. The results are shown as curve b in FIG. 2.
Referring to FIG. 2, it can be seen the gaseous sulfur compounds in the feed gas are reduced to minimal concentration by the catalyst bed of the present invention at a temperature of about 400C, while a single-layer iron-alumina catalyst bed requires temperatures above 550C to even approach minimal concentration.
Referring now to FIG. 3, therein is shown a further modification of the present invention wherein a dry gas in conduit 7 containing little or no CO is passed through acoke bed 8 at a temperature of about 500C to produce the necessary CO for the catalysis in the dual-layer bed inreactor tube 1.
One theory advanced in explanation of the present invention is that the first layer of the dual-layer bed favors the rapid production of sulfide intermediates, which rapidly react to form elemental sulfur in the presence of the catalyst in the second layer, although the improved results of the present invention are not attained when the pellets of the two layers are intimately intermixed.
What is claimed is:
l. A process for removing $0 from a dry waste gas comprising passing said waste gas through a single bed of catalyst said bed having a temperature of about 400C in the presence of CO; said CO and S0 being present in a COzSO mole ratio of at least 2:1; said bed consisting of a first and second layer of catalyst, said first layer consisting of iron, chromium, nickel, cobalt about 500C so as to produce said CO.
4. The process ofclaim 3 wherein said first layer is iron supported on alumina.
5. The process ofclaim 1 wherein said first and sec ond layers are present in a weight ratio of about 2:1.
6. The process ofclaim 4 wherein said first and second layers are present in a weight ratio of about 2: l.
Claims (6)
1. A PROCESS FOR REMOVING SO2 FROM A DRY WASTE GAS COMPRISING PASSING SAID WASTE GAS THROUGH A SINGLE BED OF CATALYST SAID BED HAVING A TEMPERATURE OF ABOUT 400*C IN THE PRESENCE OF CO, SAID CO AND SO2 BEING PERSENT IN A CO:SO2 MOLE RATIO OF AT LEAST 2:1, SAID BED CONSISTING OF A FIRST AND SECOND LAYER OF CATALYST, SAID FIRST LAYER CONSISTING OF IRON, CHROMIUM, NICKEL, COBALT OR MANGANESE SUPPORTED ON ALUMINA, SAID SECOND LAYER CONSISTING OF ALUMINA, AND WHEREIN SAID GAS ENTERS SAID BED THROUGH SAID FIRST LAYER, PASES THERETHROUGH INTO SAID SECOND LAYER, AND EXITS FROM SAID BED FROM SAID SECOND LAYER.
2. The process of claim 1 wherein said first layer is iRon supported on alumina.
3. The process of claim 1 wherein said waste gas is first passed through a coke bed at a temperature of about 500*C so as to produce said CO.
4. The process of claim 3 wherein said first layer is iron supported on alumina.
5. The process of claim 1 wherein said first and second layers are present in a weight ratio of about 2:1.
6. The process of claim 4 wherein said first and second layers are present in a weight ratio of about 2:1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US331726AUS3888970A (en) | 1973-02-12 | 1973-02-12 | Double layer catalyst bed for removing so' 2 'from waste gases |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US331726AUS3888970A (en) | 1973-02-12 | 1973-02-12 | Double layer catalyst bed for removing so' 2 'from waste gases |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US3888970Atrue US3888970A (en) | 1975-06-10 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US331726AExpired - LifetimeUS3888970A (en) | 1973-02-12 | 1973-02-12 | Double layer catalyst bed for removing so' 2 'from waste gases |
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| Country | Link |
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| US (1) | US3888970A (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3987146A (en)* | 1975-08-07 | 1976-10-19 | The United States Of America As Represented By The United States Energy Research And Development Administration | Simultaneous removal of nitrogen oxides and sulfur oxides from combustion gases |
| US4014982A (en)* | 1975-06-30 | 1977-03-29 | Texaco Development Corporation | Combined process for upgrading spent alkylation acid and reducing noxious gas content of waste gaseous streams |
| US4027001A (en)* | 1975-06-06 | 1977-05-31 | Asarco Incorporated | Process for recovering sulfur from sulfur dioxide |
| US4059673A (en)* | 1974-04-17 | 1977-11-22 | Comalco Limited | Production of bauxite and aluminium chloride of low iron content |
| US4187282A (en)* | 1976-02-12 | 1980-02-05 | Babcock-Hitachi K.K. | Process for treating a waste gas containing sulfur oxides |
| DE3219805A1 (en)* | 1982-05-26 | 1983-12-01 | Boeger Kommerz | Reactor having a catalyst for ozone breakdown |
| US4758418A (en)* | 1980-07-29 | 1988-07-19 | Union Carbide Corporation | Process for combusting solid sulfur-containing material |
| US8308848B1 (en)* | 2009-11-27 | 2012-11-13 | Tda Research, Inc. | High temperature gas desulfurization sorbents |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2631921A (en)* | 1946-08-10 | 1953-03-17 | Standard Oil Dev Co | Contacting fluid and solids |
| US2785056A (en)* | 1953-11-02 | 1957-03-12 | Metallgesellschaft Ag | Process for the production of sulfur from hydrogen sulfide and sulfur dioxide or oxygen containing gases |
| US3199955A (en)* | 1962-08-20 | 1965-08-10 | Texas Gulf Sulphur Co | Process of reducing sulphur dioxide to elemental sulphur |
| US3615219A (en)* | 1968-07-02 | 1971-10-26 | Gen Am Transport | Sulfur dioxide removal from a gas |
| US3653833A (en)* | 1969-12-09 | 1972-04-04 | Allied Chem | Processing of sulfur dioxide |
- 1973
- 1973-02-12USUS331726Apatent/US3888970A/ennot_activeExpired - Lifetime
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2631921A (en)* | 1946-08-10 | 1953-03-17 | Standard Oil Dev Co | Contacting fluid and solids |
| US2785056A (en)* | 1953-11-02 | 1957-03-12 | Metallgesellschaft Ag | Process for the production of sulfur from hydrogen sulfide and sulfur dioxide or oxygen containing gases |
| US3199955A (en)* | 1962-08-20 | 1965-08-10 | Texas Gulf Sulphur Co | Process of reducing sulphur dioxide to elemental sulphur |
| US3615219A (en)* | 1968-07-02 | 1971-10-26 | Gen Am Transport | Sulfur dioxide removal from a gas |
| US3653833A (en)* | 1969-12-09 | 1972-04-04 | Allied Chem | Processing of sulfur dioxide |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4059673A (en)* | 1974-04-17 | 1977-11-22 | Comalco Limited | Production of bauxite and aluminium chloride of low iron content |
| US4027001A (en)* | 1975-06-06 | 1977-05-31 | Asarco Incorporated | Process for recovering sulfur from sulfur dioxide |
| US4014982A (en)* | 1975-06-30 | 1977-03-29 | Texaco Development Corporation | Combined process for upgrading spent alkylation acid and reducing noxious gas content of waste gaseous streams |
| US3987146A (en)* | 1975-08-07 | 1976-10-19 | The United States Of America As Represented By The United States Energy Research And Development Administration | Simultaneous removal of nitrogen oxides and sulfur oxides from combustion gases |
| US4187282A (en)* | 1976-02-12 | 1980-02-05 | Babcock-Hitachi K.K. | Process for treating a waste gas containing sulfur oxides |
| US4758418A (en)* | 1980-07-29 | 1988-07-19 | Union Carbide Corporation | Process for combusting solid sulfur-containing material |
| DE3219805A1 (en)* | 1982-05-26 | 1983-12-01 | Boeger Kommerz | Reactor having a catalyst for ozone breakdown |
| US8308848B1 (en)* | 2009-11-27 | 2012-11-13 | Tda Research, Inc. | High temperature gas desulfurization sorbents |
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